CN100531842C - Compact distiller unit for separation of mixed fluids and distillation process for separation of such mixed fluids - Google Patents
Compact distiller unit for separation of mixed fluids and distillation process for separation of such mixed fluids Download PDFInfo
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- CN100531842C CN100531842C CNB02828531XA CN02828531A CN100531842C CN 100531842 C CN100531842 C CN 100531842C CN B02828531X A CNB02828531X A CN B02828531XA CN 02828531 A CN02828531 A CN 02828531A CN 100531842 C CN100531842 C CN 100531842C
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/06—Evaporators with vertical tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/06—Evaporators with vertical tubes
- B01D1/065—Evaporators with vertical tubes by film evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/04—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping pipe stills
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/006—Tubular elements; Assemblies of tubular elements with variable shape, e.g. with modified tube ends, with different geometrical features
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
- F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
- F28F1/14—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending longitudinally
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/14—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by endowing the walls of conduits with zones of different degrees of conduction of heat
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S203/00—Distillation: processes, separatory
- Y10S203/11—Batch distillation
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Geometry (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention relates to a compact rectifying unit for separation of mixed fluids using for heat transfer purpose a fluid heat carrier and its vapours on one of the sides of heat and mass exchanging walls. In order to increase the efficiency of the heat and mass exchange process, the heat and mass exchange tubes of the rectifying part and/or of the evaporator part have means to provide irregular (varying) amounts of heat transfer between the inside and the outside of tube wall along the height of said heat and mass exchange tubes. This allows to reduce the rectification column height by 3-10 times.
Description
Technical field
The present invention relates to a kind of small-sized distilling apparatus that fluid-mixing is separated of being used for, a kind of evaporimeter tower with heat and mass exchange pipe that is used for distilling apparatus is with a kind of distil process that fluid-mixing is separated of being used for.
Background technology
Conventional column comprises that the work of membrane type tower is: the top of the wet reflux in the reflux accumulator beyond heat between steam and liquid and the mass exchange district being taken to tower.Therefore, on all height of tower, steam flow G and liquid backflow L are constant.Liquid reflux stream amount L obviously surpasses the flow P (see figure 1) of distillation sample usually.
In a kind of membrane type tower in being similar to the present invention, liquid backflow L directly forms in all height in heat and mass exchange district.It is that each height at tower obtains by the thermograde that heat exchange walls produces that this liquid refluxes, and as a kind of film along heat exchange walls toward dirty.Therefore, these terms are defined as steam G1 and carry out forced condensation at the height h1 of desirable separation phase.When steam G1 puts the position condensation at this, form a kind of liquid backflow L1 simultaneously, and form secondary steam stream G2 (see figure 2) by the light component enrichment of mixture by the enrichment of mixture nonvolatile component.This process is carried out repeatedly along the height of tower, until the distillation concentration that reaches desired stock blend light component.
Goal of the invention
The objective of the invention is to improve the efficient of heat and mass exchange process.
According to the present invention, a kind of distilling apparatus that fluid-mixing is separated of being used for that comprises destilling tower is provided, described distilling apparatus comprises: a shell, the vapor phase outlet device at destilling tower top, the fluid phase outlet device of destilling tower bottom, tube end sheet, at least one heat and the mass exchange pipe of destilling tower are fixed between the tube end sheet, and tube end sheet keeps above-mentioned heat and the mass exchange pipe inside at shell, be used to evaporate the evaporator of above-mentioned fluid-mixing, and the device that heats above-mentioned fluid-mixing, the inner space of above-mentioned heat and mass exchange pipe is connected with above-mentioned evaporator, the aforementioned tube end plate, above-mentioned heat and mass exchange pipe and above-mentioned shell define the annular gap between the outer shell-and-tube, annular gap between above-mentioned heat and mass exchange pipe and the above-mentioned shell is filled by heat-carrying agent fluid and steam thereof, and be connected with reflux condenser and the device that heats above-mentioned heat-carrying agent, it is characterized in that above-mentioned destilling tower has the device that the heat transfer profile of irregular variation is provided between the outside in its tube wall along heat and mass exchange pipe height.
According to the present invention, an irregular thermograde is arranged between heat exchange tube wall both sides along tower height.By the heat exchange tube wall, and/or have a kind of irregular thermal power transfer at least between the gas phase of heat-exchange tube one side and liquid phase, one of its result forms a kind of irregular liquid that is complementary with the distillate performance along tower height to reflux.
The heat accumulation of the heat-carrying agent of the surplus heat when liquid reflux to form by consuming outside boiling and by heat and the discharge of mass exchange surface wall, and outside heat-carrying agent is in the space of opposite side of above-mentioned heat and mass exchange surface wall.
The present invention can make the height of the desired separated level in the membrane type tower reach lower value, reaches in the tower and the high useful load of the corresponding vapor flow rate of industrial packed column useful load.In actual applications, this can make distillation tower height be reduced to 1/3-1/10, compares with conventional column, and this can make, and parting material content is reduced to 1/50-1/100 in the tower.
As everyone knows, the heat conduction by heat and mass-heat exchange tube wall can have bigger variation along its tower height degree with along heat and mass exchange pipe respectively.Evaporate in inside or heat and the mass exchange pipe or the component of condensation fluid-mixing though be preferably in, and in annular gap, provide a kind of heat-carrying agent fluid around above-mentioned heat and mass exchange pipe, but in principle, within the scope of the present invention, can be at above-mentioned heat and mass exchange pipe external evaporation and/or the above-mentioned fluid-mixing of condensation, and by importing the heat-carrying agent fluid in the pipe.
And importantly, for the present invention, heat exchange not only takes place in heat and mass exchange tube wall both sides, and can take place between the mixing constituent element and/or between the gas phase of fluid-mixing and the liquid phase.
At last, important also is, the mass exchange of fluid-mixing component can promptly take place from heat and mass exchange tube wall surface a distance at the steam flow center, and/or also can take place between the liquid thin fluid film on gas phase and above-mentioned heat and the mass exchange tube wall surface.
One of special advantage of the present invention is can be to widely, the almost hard-core fluid-mixing of scope efficiently distills.The boiling temperature of fluid-mixing particularly to be separated and condensation and evaporation can or each component needn't be interrelated.Using a kind of itself also is that the fluid-mixing and the heat-carrying agent fluid of working between vapor phase and liquid phase provide a kind of efficient way, with in very wide scope along the Level Change heat of its heat and mass exchange pipe and the heat transmission between the mass exchange tube wall both sides.Though the temperature of heat and mass exchange tube wall highly can be constant along it, this temperature preferably highly has big variation along it, so that form irregular heat transfer profile along heat and mass exchange pipe height.Height along heat and mass exchange pipe forms a kind of special backflow distribution simultaneously, this backflow is preferably irregular, not constant promptly along its heat and mass exchange pipe height, this will be in each distillation stage, promptly, keep the balance between steam and the liquid at the differing heights of heat and mass exchange pipe.
Description of drawings
Fig. 3 illustrates, owing to descend (from bottom to top) along the heat and the height H thermograde of mass exchange pipe 2, the heat transmission is irregular, at the irregular liquid backflow form L of the distillation fraction 12 of destilling tower 13.
Fig. 4 illustrates, owing to evenly raise (from bottom to top) along the heat and the height H thermograde of mass exchange pipe 2, the heat transmission is irregular, at the irregular liquid backflow form L of the distillation fraction 12 of destilling tower 13.
Fig. 5 illustrates, because along the heat and the inhomogeneous decline of height H thermograde (from bottom to top) of mass exchange pipe 2, the heat transmission is irregular, at the another kind of irregular liquid backflow form L of the distillation fraction 12 of destilling tower 13.
Fig. 6 illustrates, because along the heat and the inhomogeneous rising of height H thermograde (from bottom to top) of mass exchange pipe 2, the heat transmission is irregular, at the another kind of irregular liquid backflow form L of the distillation fraction 12 of destilling tower 13.
Fig. 7 illustrates the design that the destilling tower 10 of irregular fever transmission and irregular backflow form is provided along the height of heat and mass exchange pipe 2.
Fig. 8 illustrates the design of second kind of remodeling of a tower (distillation fraction).
Fig. 9 and Fig. 9 a illustrate the third remodeling of a tower (distillation fraction).
Figure 10 illustrates along some examples of the irregular section of the rib of heat and the arrangement of mass exchange tube outer surface.
Figure 11 illustrates the 4th kind of remodeling of a tower (distillation fraction).
Figure 12 illustrates the 5th kind of remodeling of a tower (distillation fraction).
Figure 13 illustrates the 6th kind of remodeling of a tower (distillation fraction).
Figure 14 illustrates the process chart according to a tower that manufactures and designs of above-mentioned membrane type tower.
Figure 14 a illustrates the process chart of the condensation of gas destilling tower in Verkh-Tatarskoye oil field, Siberia.
Figure 15 illustrates the design development of destilling tower 8 (Figure 14, the view 1 of 14a).
Figure 16 illustrates Figure 14, destilling tower evaporimeter among the 14a.
Figure 17 is illustrated in the design development that vapor space is introduced this evaporimeter of cross section perforation dividing plate 408.
Figure 18 illustrates the process chart of productivity ratio without any a kind of tower of restriction.
Figure 19 illustrates the design of membrane type stripping evaporimeter.
Figure 20 illustrates the another kind remodeling of membrane type stripping evaporimeter.
Figure 21 illustrates the third remodeling of membrane type stripping evaporimeter.
The specific embodiment
According to Fig. 7, destilling tower 10 comprises the housing 1 with tube end sheet 3 and 4, and heat and mass exchange pipe 2 are fixed between the tube end sheet.In the bottom of the distillation fraction 12 of destilling tower 10, the throttle pipe (inlet tube) 6 that has 7 and one of the throttle pipes (outlet/inlet pipe) of an input heat-carrying agent that the heat-carrying agent condensate liquid is returned.At the top of destilling tower, there is one the heat-carrying agent vapor phase drawn and make the jet pipe (outlet/inlet pipe) 5 that the heat-carrying agent condensate liquid returns.
The work of this destilling tower is as follows: fill annular gap 100 with a kind of heat-carrying agent by throttle pipe 7.Heat-carrying agent in the distillation fraction 12 (tower section) can be that its boiling point arrives than low boiling distillation boiling point (T at mixture initial mixing boiling point to be distilled
B1) any liquid or the fluid-mixing of scope.Heat-carrying agent in the stripping part (tower section) can be any liquid or the fluid-mixing of its boiling point in mixture initial boiling point to be separated arrives residue higher constituent element boiling spread.(stripping partly is discussed later)
Heat-carrying agent thisly is condensate in heat and mass exchange pipe 2 inner wall surface take place or take place to consume the heat of importing from outer thermal source by housing 1 under the condensation heat effect of the steam of distillating liquid and seethe with excitement.The heat-carrying agent steam rises in annular gap 100, and distributes reflux condenser (not shown) of importing at a joint or jet pipe 5.The heat-carrying agent distillate passes through joint or jet pipe 5 from this reflux condenser again, and/or turns back to the annular gap of tower by throttle pipe 6.Therefore, prevented that heat-carrying agent from leaking from tower.Carry out the level control of the heat-carrying agent that seethes with excitement in the tower by gate throttle or joint 7, provide its thermograde at the differing heights of heat and mass exchange pipe 2.Therefore, along the distribution of heat and mass exchange pipe 2 height, provide this gradient with the temperature difference of the boiling-point difference on the stationary fluid height in the tower, steam and liquid and steam thereof and liquid.
According to above-mentioned explanation,, form a kind of liquid and reflux at inner surface of tube wall.This backflow is past dirty along tube wall with a kind of form of film.The steam of distillating liquid rises to the top of pipe 2.Along the height of pipe 2, at the steam flow that rises with toward heat and mass exchange process take place between the dirty liquid backflow film.The vapor phase of the cleaning of distillating liquid flows out the pipe top so that condensation and cooling.Liquid refluxes and to remove from tower bottom heat and mass exchange pipe, perhaps as target fraction, perhaps flow into tower than the lower part, perhaps flow into the stripping part of tower.
Be the adjusting that thermograde is added, the method that can adopt industrial department to adopt is equipped with a pressure regulator (not shown) on this reflux condenser.Pressure in the annular gap 100 raises or reduces the boiling point that all changes heat-carrying agent, and changes the thermograde between heat-carrying agent steam and the liquid.
Be shown in similar described in a kind of alternate design of tower of Fig. 8 and Fig. 7.Its difference is: at first, at the annular gap top, vapor outlet port and heat-carrying agent condensate liquid return below the district, are provided with a distribution plate 8; Secondly, the wall thickness of heat and mass exchange pipe is along its alterable height.As Fig. 3, the example in 4,5 or 6 is such, and the variation of wall thickness is determined by desired liquid backflow form.Fig. 8 illustrates a kind of remodeling of the pipe thickness of heat and mass exchange pipe 2 towards the bottom increase.
The work of tower is as follows: the steam of the heat-carrying agent of boiling rises at annular gap 100, and enters a reflux condenser by a joint or jet pipe 5.The distillation condensate liquid returns and drops on the above-mentioned distribution plate 8 by above-mentioned joint 5.Therefore, this condensate liquid is begun to heat by the countercurrent vapor on jet pipe 5 and the distribution plate 8.One deck condensate liquid 9 flow through above-mentioned distribution plate 8 base plates and pipe between 2 the gap and as thin film at the outer surface of pipe 2 toward dirty.This condensate liquid film toward current downflow is also heated by the heat-carrying agent steam flow toward rising.Along the height of tower, the conduction of the irregular fever of the wall of heat and mass exchange pipe 2 provides origin for thermograde.Simultaneously, as previously described, also realized (level) thermograde.The condensation portion of heat-carrying agent also can be returned by a joint or throttle pipe 6.The inboard generation heat of the pipe 2 in the tower and the explanation of mass exchange and front are similar.
Embodiment among Fig. 9 and the 9a and aforementioned schemes difference are: heat and mass exchange pipe 2 are constant along its height wall thickness.Simultaneously, the outer surface at pipe 2 has the rib of some its cross sections along alterable height.In this remodeling, realize its thermograde along highly irregular shape by these ribs.The more erose examples of rib are shown in Figure 10:
(a) the rib width increases towards the bottom.
(b) the rib width reduces towards the bottom.
(c) the rib width diminishes towards the middle part.
(d) rib width inhomogeneous increase towards the bottom.
(e) rib width inhomogeneous reduction towards the bottom.
(f) different with the degree of depth because of the width of groove, rib is heterogeneous along the heat conduction of its height.
(g) because the hole of different-diameter and in the non-uniform Distribution of rib surface, the heat conduction of rib is heterogeneous.The work of this tower and the scheme of front are similar.
The 4th embodiment and aforementioned schemes difference among Figure 11 are, realize irregular thermograde without rib, and adopt and outer tube 16A hot and 2 coaxial installations of mass exchange pipe and maintenance certain distance.Be equipped with some holes 11 on the outer tube 16A, hole number is along its height non-uniform Distribution.Heat and mass exchange pipe 2 outer surfaces are along its highly irregular hot transition status, have realized along the scrambling of the thermograde of the height of hot and mass exchange pipe 2.For example, Figure 11 illustrates a kind of remodeling of the quantity increase in hole from top to bottom.The work of tower and the scheme of front are similar.
The 5th embodiment shown in Figure 12 and aforementioned type difference be, heat and mass exchange pipe 2 by from a distance with one heart installation, along its pipe 16B that highly has an irregular cross section (open pipe flow region) around.On bottom and the top of pipe 16B, be useful on heat-carrying agent is introduced heat and mass exchange pipe 2 and the hole 11 that is used for discharging from the top its steam.To manage 2 outer surfaces, realize along the scrambling of the thermograde of heat and mass exchange pipe 2 height along its highly irregular hot transition status.This scrambling particularly realizes by the velocity gradient of the mobile heat-carrying agent steam of the surrounding tube 2 and the variable gap of pipe 16B formation.For example, Figure 12 illustrates a kind of remodeling that opening flow region from top to bottom reduces.
The operation class of this tower is similar to aforesaid type.
The 6th kind of design class of the tower shown in Figure 13 is similar to design shown in Figure 8, and difference is: use a kind of external heat chamber 611 to make the heat-carrying agent boiling.The heat-carrying agent liquid level is preferably lower than tube end sheet 4.Heat-carrying agent in the heating clamber 611 is for example by a sleeve, to consume by this chamber walls from the heat of extraneous thermal source input seethe with excitement (not shown extraneous thermal source).Heating clamber 611 is connected with housing 1 bottom by a joint or throttle pipe 6, and is connected with tube end sheet 4 by a tube connector 610.A passage 7B that heat-carrying agent is passed through is arranged in tube end sheet 4.The heat-carrying agent steam rises to the annular gap 100 of tower by tube connector or throttle pipe 6, and the heat-carrying agent condensate liquid turns back to heating clamber by passage 7B and tube connector 610.The work and the aforementioned type of this tower are similar.With shown in Figure 8 the same, the thickness of the wall of pipe 2 reduces from bottom to top.
To the irregular wall thickness of heat and mass exchange pipe 2, irregular rib, the shell of uneven shell with holes and/or variable cross-section makes up, and can also constitute different remodeling.
As shown in figure 14, a kind of destilling tower of the present invention is made of following main device: preheater 302, preheater 304, evaporimeter 306, furnace chamber 307, destilling tower 308, condenser 310, separator 311, reflux condenser 326.
Example 1
Siberia Verkh-Tarskoye crude oil distillation
The work of tower is as follows.Prepare the oil that is used to distill by standard technology in advance.Flow by 1250kg/h (kilogram/hour) goes out oil tank to crude oil pump, is transported to the annular gap of shell-and-tube type preheater 302 by oil pipe 301.Crude oil temperature is 10 ℃.Temperature is 250 ℃ diesel oil is transported to preheater 302 by pipeline 313 from destilling tower tubular space.By the diesel oil of Quench to 50 ℃ conversely heating crude oil to 60 ℃.Be heated the vapor phase of oil, comprise that uncondensable unstripped gas directly is transported to condenser 310 from preheater 302 tops by pipeline 317.Also have another kind of possible remodeling, promptly Crude Oil Transportation to the tubular space of preheater 302 with diesel oil is transported to the annular gap of preheater 302.
The fluid communication piping 303 that is heated crude oil is transported to the annular gap of shell-and-tube type preheater 304.Temperature is 360 ℃ dirty oil is transported to preheater 304 by pipeline 315 from the stripping part of evaporimeter 306 tubular space.By Quench to 95 ℃, the temperature of dirty oil Convective Heating crude oil to 129 ℃.Also can be transported to above-mentioned annular gap to Crude Oil Transportation to the above-mentioned tubular space of preheater 304 with dirty oil.
Heated crude oil enters the annular gap 341 of evaporimeter 306 start-up portions by pipeline 305.In this evaporimeter, crude oil is by the advection heat combustion gas heating of introducing from furnace chamber 307 by heating tube 340.At the start-up portion of heater 306, crude oil is heated to 360 ℃.Heating-up temperature by evaporimeter 306 start-up portions is controlled the conveying of crude oil, and this start-up portion also is a stripping part of destilling tower 308 simultaneously.Partly being heated to 360 ℃ this dirty oil cut by evaporimeter 306 strippings is transported to above-mentioned preheater 304 and cools off.Flue gas is rejected to chimney 337 by pipeline 321 from evaporimeter.
In destilling tower 308 with heat and mass exchange pipe 350, heat and mass exchange process take place, its result, light hydrocarbon vapor are separated into the fluid phase of diesel oil distillate and the vapor phase of gasoline fraction.The height of the heat of destilling tower 308 and mass exchange part is 1.5m (rice).Diesel oil is discharged destilling tower with 220-270 ℃ temperature from cracking dish 320, enters above-mentioned preheater 302 and cools off.Temperature is that 110-120 ℃ gasoline fraction steam is transported to condenser 310.In the annular gap 100 of destilling tower 308, such (Fig. 7-13) as the aforementioned, the heat-carrying agent boiling is for hot and mass exchange pipe provide high validity.For example, the mixture of high-quality ethanol and water is as a kind of heat-carrying agent.A part of furnace gas from pipeline 321 is transported to by pipeline 322 in the sleeve 323 of tower 308 bottoms, and heat is transferred to heat-carrying agent in the annular gap 100.This extra input heat is regulated by operated door 342.Flue gas is discharged to chimney 337 from sleeve 323 by flue gas leading 324 and 321 then.At the top of annular gap 100, the heat-carrying agent steam enters reflux condenser 326 by tracheae 325.The heat-carrying agent condensate liquid turns back in the tower by pipeline 325 and/or pipeline 327.Utilize valve 328, pipeline 327 can partly or fully overlap.Heat-carrying agent in the tower 308 is by through pipeline 339 it being input to holding vessel 338 or discharging holding vessel 338 and regulate.Return condensed device 326 is communicated with atmosphere by a pressure regulator 343.Adjuster 343 provides a pressure below atmospheric pressure or a higher pressure in annular gap 100.Change along with above-mentioned adjuster 343 makes above-mentioned pressure, the heat-carrying agent temperature in the tower 308 is changed.
The gasoline fraction steam at tower 308 tops is transported to condenser 310 by pipeline 309.Gasoline fraction condensation here and be cooled to 30-50 ℃.Cooling gasoline enters separator 311 from condenser 310.
In separator 311, from the gasoline fraction of disposing, isolate unstripped gas and condensed water.Condensed water is discharged to furnace chamber 307 from separator 311 bottoms by pipeline 334 with the flow of 3kg/h (kilogram/hour).In furnace chamber, condensed water is by helix tube 335 circulations.Here condensate evaporation is transported to furnace chamber as steam, is used for the fire prevention of residual hydrocarbon, and is retained in the initial condensation water.The unstripped gas at separator 311 tops is transported to the fire-proofing 330 of combustion chamber 331 by pipeline 329, is used for playing liquefaction at furnace chamber 307.Raw gas flow is 48kg/h (kilogram/hour).Do not pump separator 311 and be input to oil tank with the flow of 414kg/h by pipeline 312 with the gentle gasoline that combines of water.
Cooling diesel oil pumps by pipeline 314 from preheater 302 and is input to oil tank with the flow of 454kg/h.The cooling dirty oil pumps by pipeline 316 from preheater 304 and is input to oil tank with the flow of 331kg/h.
Example 2
Siberia Verkh-Tatarskoye oil field gas-condensate liquid distillation
The flow chart of tower such as Figure 14 a, the work of tower is as follows: condensate liquid flow with 1000kg/h from a holding vessel (not shown) pumps, and enters the annular gap of shell-and-tube type preheater 302 by pipeline 301.Temperature is 220-240 ℃ furnace oil is imported preheaters 302 by pipeline 315 from evaporimeter 306 tubular space.Quench to 40 ℃, furnace oil is heated to 31 ℃ to gas-condensate liquid by convection current.The vapor phase of heated gas-condensate liquid comprises uncooled unstripped gas, directly gets rid of from preheater 302, enters condenser 310 by pipeline 317.Also can be transported to gas-condensate liquid the tubular space of preheater 302, furnace oil is transported to annular gap.
Heated gas-condensate liquid is input to the annular gap 341 of evaporimeter 306 start-up portions by pipeline 305.In evaporimeter, gas-condensate liquid is by the advection heat combustion gas heating of transmitting from furnace chamber 307 by heating tube 340.In the decline of evaporimeter 306, the temperature of gas-condensate liquid is 220-240 ℃.Gas-condensate liquid carries control to press evaporimeter 306 back-page heating and temperature control, and evaporimeter decline is a stripping part of tower simultaneously.The light hydrocarbon vapor of evaporimeter 306 is input to tower 308, partly is heated to 220-240 ℃ furnace oil cut by evaporimeter 306 strippings and is transported to preheater 302 and cools off.Flue gas is got rid of by pipeline 321 from evaporimeter and is entered chimney 337.
In tower 308 with heat and mass exchange pipe 2, heat and mass exchange process take place, thus, light hydrocarbon vapor is separated out from suitable diesel oil distillate fluid mutually and the gasoline fraction vapor phase.The height of heat in the tower and mass exchange part is 1.5m.The diesel oil of light fraction turns back to evaporimeter 306, and gets rid of in this structure with the furnace oil cut, enters preheater 302 so that further cool off by pipeline 315, and temperature is 105-115 ℃ a gasoline fraction input condenser 310.The work of tower 308 and aforesaid similar.
The gasoline fraction at tower 308 tops is input to condenser 310 by pipeline 309.Gasoline fraction condensation here and be cooled to 30-35 ℃.The gasoline of cooling is transported to separator 311 from condenser 310.
In separator, unstripped gas separates from handle gasoline fraction with condensed water.Condensed water is got rid of from separator 311 bottoms, enters furnace chamber 307 with the flow of 2.5kg/h by pipeline 334.In furnace chamber, condensed water is by helix tube 335 circulations.Condensed water here evaporates, and is input into furnace chamber as steam, is used for the fire prevention of residual hydrocarbon, and is kept in the initial condensed water.Flue gas enters the fire-proofing 330 of furnace chamber 307 combustion chambers 331 by pipeline 329 from separator 311 tops.Raw gas flow is 58kg/h.Do not pump separator 311, enter holding vessel by pipeline 312 with the flow of 826.5kg/h with the gentle gasoline that combines of water.
The furnace oil of cooling pumps from preheater 302, enters oil tank by pipeline 314 with the flow of 103kg/h.
The work of furnace chamber 307 as previously mentioned.
Figure 15 illustrates the design development (Figure 14, the view I of 14a) of destilling tower 308
(a) in order to produce maximum thermograde along distillation tower height, tower can be formed a kind of heat-carrying agent of each section employing different boiling by two sections or multistage.
(b) in order to select the intergrade cut of destilling tower, tower can be made up of two sections or multistage, and each section all is useful on gets rid of the pallet that gold-plating divides.
(c) in order to obtain the effective status of still-process, steam and proportional the reducing of fluid flow mutually in the tower in total circulation area of heat of every next section and mass exchange pipe and the tower.
Figure 14, the evaporimeter of the tower shown in the 14a have shown a kind of shell-and-tube type heat exchanger (Figure 16).At the butt end of shell 401, settle tube end sheet 402 and 403, heating tube 404 is fixed on the tube end sheet.The location of heating tube makes housing 401 tops that a standby annular gap be arranged.The outlet 405 that is connected with destilling tower is positioned at the evaporimeter edge, near tube end sheet 402.Near tube end sheet 402 places, arrange an outlet connection 407 that is used to get rid of the stripping residue in shell 401 bottoms.Near tube end sheet 403 places, there is an inlet union 406 to be used for raw material is input into evaporimeter in a relative side.Inlet union 406 can be placed in housing 401 bottoms, or is placed in medium (not shown) gas-liquid interface layer place.The work of this evaporimeter is as follows.Raw material (as oil) is input into evaporimeter by inlet union 406, is filled into annular gap, covers heating tube.At the evaporimeter top, there is a space to be used for steam and passes through.Be not input into the situation of the raw material of heating at evaporimeter, joint is positioned at the bottom.Raw material in heating is the situation of vapor phase, and inlet union 406 is positioned at the gas-liquid interface layer of medium.Oil flows in the direction towards outlet 405 along heating tube 404.Hot flue gases flows to heating tube from furnace chamber (not shown Figure 16) along opposite direction, is rejected to chimney gatherer (Figure 16 is not shown) from the opposite side of evaporimeter then.Therefore, in evaporimeter, realize the convective heat exchange that oil is gentle.Because oil is slowly heated in convective motion, formed light hydrocarbon evaporation.In the end (right side of Figure 16) of evaporimeter, oil is heated to the maximum temperature of selected cut.Therefore, have only dirty oil still to be retained in the zone of end plate 402 with liquid form.Therefore, the decline of evaporimeter also is a stripping part of tower simultaneously.After this, dirty oil flows to outlet connection 407 from the evaporimeter eliminating immediately.Oil is no more than a few minutes in the retention time of maximum temperature, therefore, can not produce carbon on the surface of heating tube 404.The slow variation of oil boiling point and even raising impel the effective extraction of light hydrocarbon fraction.Evaporation process at the beginning, and is mobile by the evaporimeter free space abreast in the oil meter face direction of tower from the light hydrocarbon fraction steam of oil evaporation.Therefore in flowing, it meets with the high boiling fraction steam.As the steam results of interaction, the stripping of vapor phase takes place.In the end of evaporimeter, steam rises to outlet 405, and then enters destilling tower.
Figure 17 illustrates the design development of this evaporimeter, and difference is to introduce cross section dividing plate 408 with holes at evaporating space.
In fact these dividing plates are immersed in the ebullated bed of oil.The hydrocarbon vapor of evaporating from oil produces eddy current by dividing plate.Hydrocarbon vapor stream is crossed dividing plate with holes, has improved steam stripping efficiency in baffle surface and the space between dividing plate.
The quantity of heated oil is few in evaporimeter.For example, for the evaporator capacity of the tower of annual 10000t (ton), output is 400L (liter) oil.Because the hydrocarbons content in evaporimeter and the membrane type tower is little, therefore, might be combined into tower, evaporimeter, furnace chamber a kind of integral body, compact single structure device and don't runs counter to fire prevention and explosion safety standard.
The design of the tower that Figure 14,14a introduce can become that to handle raw material in a kind of year be 100000-150000t (ton) ability, a complete set of distillation equipment of high performance compactness.
Figure 18 illustrates the process chart of a kind of productive rate without any the tower of restriction.The characteristics of this tower are that a membrane type stripping evaporimeter 306a is arranged.The oil of heating is transported to the top of evaporimeter 306a by pipeline 305, and as film at heating tube 340a inwall toward dirty.The furnace gas of furnace chamber 307 is transported to annular gap 341a via distribution gatherer 344, and gets rid of from evaporimeter by pipeline 321.Toward current downflow the time, film is heated.Light hydrocarbon fraction and enters destilling tower 308 from evaporation here.Remaining liquid dirty oil cut down flows to into the stripping part, and is rejected to preheater 304 by pipeline 315.The evaporimeter stripping partly has a heating muff 347.Part flue gas is discharged from furnace chamber 307, enters heating muff 347 via pipeline 345.Flue gas is passed through pipeline 347, and gets rid of via pipeline 345a.The temperature of stripping part is regulated via operated door 348 control gas flows.Evaporimeter detailed structure and working procedure will be narrated below.In addition, tower with the similar mode of aforementioned tower work (seeing Figure 14).
Compare with aforesaid evaporimeter type (Figure 16), using kestner long-tube evaporator can make the content of heating oil be reduced to 1/50-1/100 combines with the membrane type tower, might be combined into constructional device a kind of integral body, compact, single to tower, evaporimeter and furnace chamber, and without prejudice to fire prevention and explosion safety standard.
The design of the tower that Figure 18 introduces can obtain a kind of high performance, compact, can handle any raw material (condensate liquid or its mixture of oil, gas, or other liquefied mixtures), productive rate is without any a complete set of distillation equipment of restriction.
Figure 19 illustrates the design of membrane type stripping evaporimeter.
This evaporimeter is made of vertical shell 1 and tube end sheet 503 and 504, and heating tube 2 is fixed between the pipe end.In the bottom of shell 1, arranged to have the distribution gatherer 506 of window 507.Gatherer 506 has a tube connector 505 to be used to import waste gas.On window 507, arrange to have the lower clapboard 509 in hole 508, these holes and heating tube 2 are coaxial and diameter is close.At the top of shell 1, arrange a gatherer 506a with window 507a.Gatherer 506a has a tube connector that is used to scavenge 510.Below window 507a, arrange to have the upper spacer 509a of hole 508a, these holes are concentric with heating tube 2.At the top, a connector 511 is attached to and is used on the tube end sheet 503 being connected with destilling tower.Connector 511 has a pipe joint 512, is used for raw material is transported to deflector 513.Cube 514 with sleeve 516 is connected down on the tube end sheet 504.In this cubical bottom, a pipe joint 515 that is used to drain the stripping residue is arranged.Sleeve 516 has the pipe joint 517 of an input waste gas and the pipe joint 518 of an output flue gas.
This evaporator operation is as follows: raw material (as oil) is transported to the surface of tube end sheet 503 by pipe joint 512.Deflector 513 makes oil distribute on the tube end sheet surface.This oil is past dirty at the inner surface of heating tube 2 as film.Furnace chamber waste gas is transported to gatherer 506 from the furnace chamber on the tube connector 505, and is evenly distributed on by window 507 in the annular gap of shell 1.Flue gas is passed dividing plate 509 via hole 508 and is risen, to heat the outer surface of this pipe 2.Hole 508 makes flue gas evenly move along heating tube 2.This causes the uniform vertical temperature gradient along the evaporimeter height.Via hole 508a and window 507a, the flue gas of cooling enters gatherer 506a from the annular gap eliminating of shell 1.They are further got rid of by tube connector 510.As the result of the heat exchange of this convection current (reverse flow), oil film is heated, and light hydrocarbon fraction is discharged.Hydrocarbon vapor rises along pipe 2, and interacts with past dirty liquid film.Heat and mass exchange take place in the result between them.Fry dried food ingredients is given birth to stripping.Still stay the heating tube top from the hydrocarbon vapor that high boiling fraction is refining.Steam enters destilling tower from connector 511.In the bottom of heating tube 2, when only remaining dirty oil in the liquid phase, oil film is heated to the maximum temperature of selected cut.Oil film flows to a cube 514 downwards, and here the dirty oil cut is excluded by pipe joint 515.Part flue gas is transported to sleeve 516 with heating cube 514 via pipe joint 517.Waste gas in the sleeve is excluded by pipe joint 518.
Carry out the input of oil and flue gas in such a way: make liquid film be heated to the maximum temperature of selected cut in the heating tube bottom.Heating-up temperature is by the temperature check of dirty oil in the cube.When critical-temperature, oil the evaporimeter time of staying be no more than 1min (minute).
Figure 20 illustrates the another kind remodeling of membrane type stripping evaporimeter.
The design of this remodeling and work are as previously mentioned.From distributing the zone of gatherer 506 input waste gas, heating tube 2 by the concentric sleeve 519 that keeps a distance around.Between heating tube 2 and sleeve 519, an annular gap is arranged.Sleeve 519 separates the heating tube bottom with hot furnace gas, therefore prevented to manage the danger that 2 lower inner surface dirty oil films are burnt.Heating tube 2 between dividing plate 509 and 509a is arranged in the confinement tube 520 of concentric installation, therefore, and for providing more high efficiency heat exchange between flue gas and the heating tube 2.For further improving heat exchanger effectiveness, heating tube 2 can be provided with a kind of horizontal or vertical fin (not shown).
Figure 21 illustrates the third remodeling of membrane type stripping evaporimeter.
The design of this remodeling and work and aforementioned type are similar.Fill with a kind of heat-insulating material or liquid fillers annular gap at sleeve 519 and heating tube 2, and the fusing point of liquid fillers is no more than the temperature range from the substrate mixture decomposition temperature to stripping residue decomposition temperature.In the situation that furnace gas flow and temperature are sharply jumped and changed, the liquefaction filler in the gap begins fusing.The temperature of pipe bottom is stablized, prevented technology controlling and process in the time dirty oil film burnt.Pallet 522 of direct configuration below following tube end sheet 504.The dirty oil film flows downstream in the pallet, has therefore covered the edge of cube 514 bottoms.Via introducing this pallet, it is possible that the dirty oil maximum heating temperature is additionally controlled.
Label list
1 housing
2 heat and mass exchange pipes
3 tube end sheet
4 tube end sheet
5 jet pipes
6 throttle pipes
7 throttle pipes
The 7B passage
8 distribution plates
9 condensation liquid layers
10 ribs
11 holes
12 distillation fractions
13 destilling towers
14 stripping parts
15 ribs
The 16A outer tube
The 16B outer tube
100 annular gaps
110 destilling towers
112 distillation fractions
114 stripping parts
114A heat and mass exchange pipe
301 pipelines
302 preheaters
303 pipelines
304 preheaters
305 pipelines
306 evaporimeters
306A membrane type stripping evaporimeter
307 furnace chambers
308 destilling towers
309 pipelines
310 condensers
311 preheaters
312 pipelines
313 pipelines
314 pipelines
315 pipelines
316 pipelines
317 pipelines
320 cracking dishes
321 pipelines
322 pipelines
323 sleeves
324 pipelines
325 pipelines
326 reflux condensers
327 pipelines
328 valves
329 pipelines
330 fire-proofings
331 combustion chambers
332 igniter chambers
333 pipelines
334 pipelines
335 helix tubes
336 operated door
337 chimneys
338 holding vessels
339 pipelines
340 heating tubes
The 340A heating tube
341 annular gaps
The 341A annular gap
342 operated door
343 pressure regulators
344 distribute gatherer
345 pipelines
The 345A pipeline
346 operated door
347 heating muffs
348 operated door
401 shells
402 tube end sheet
403 tube end sheet
404 heating tubes
405 outlets
406 inlet union
407 outlet connections
408 cross sections dividing plate with holes
503 tube end sheet
504 tube end sheet
505 tube connectors
506 gatherers
The 506A gatherer
507 windows
The 507A window
508 holes
The 508A hole
509 lower clapboards
The 509A upper spacer
510 connectors
511 connectors
512 pipe joints
513 sleeves
514 cubes
515 pipe joints
516 sleeves
517 pipe joints
518 pipe joints
519 concentric sleeves
520 confinement tube of installing with one heart
521 heat-insulating materials
522 pallets
610 tube connectors
611 outer heating clambers
The G steam flow
The h1 transport disengaging height
L liquid refluxes
P distills sampling
Claims (35)
1. distilling apparatus that fluid-mixing is separated of being used for that comprises destilling tower, described distilling apparatus comprises:
(a) shell,
(b) the vapor phase outlet device at destilling tower top,
(c) the fluid phase outlet device of destilling tower bottom,
(d) tube end sheet, at least one heat and the mass exchange pipe of destilling tower are fixed between the tube end sheet, and tube end sheet keeps above-mentioned heat and mass exchange pipe in the inside of shell,
(e) be used to evaporate the evaporator of above-mentioned fluid-mixing, and the device that heats above-mentioned fluid-mixing,
The inner space of above-mentioned heat and mass exchange pipe is connected with above-mentioned evaporator,
Aforementioned tube end plate, above-mentioned heat and mass exchange pipe and above-mentioned shell define the annular gap between the outer shell-and-tube,
Annular gap between above-mentioned heat and mass exchange pipe and the above-mentioned shell is filled by heat-carrying agent fluid and steam thereof, and is connected with reflux condenser and the device that heats above-mentioned heat-carrying agent,
It is characterized in that above-mentioned destilling tower has the device that the heat transfer profile of irregular variation is provided between the outside in its tube wall along heat and mass exchange pipe height.
2. according to the described distilling apparatus of claim 1, it is characterized in that, above-mentioned evaporator is made for a kind of shell-and-tube type heat exchanger, a chamber of described heat exchanger is connected with the inner space or the annular gap of above-mentioned destilling tower, and the chamber of other of described heat exchanger is connected with the device of the above-mentioned fluid-mixing of heating.
3. according to claim 1 or 2 described distilling apparatus, it is characterized in that the heater that heats above-mentioned fluid-mixing is a stove, with a sleeve of an above-mentioned evaporator that is connected with above-mentioned stove.
4. according to each described distilling apparatus among the claim 1-2, it is characterized in that the heater that heats above-mentioned heat-carrying agent is a stove and a sleeve that is connected with this stove.
5. according to each described distilling apparatus among the claim 1-2, it is characterized in that the said apparatus that above-mentioned irregular heat transfer profile is provided is the liquor-level regulator of the heat-carrying agent fluid in the annular gap of above-mentioned destilling tower.
6. according to each described distilling apparatus among the claim 1-2, it is characterized in that, be used for pressure regulator of reflux condenser configuration of above-mentioned heat-carrying agent.
7. according to each described distilling apparatus among the claim 1-2, it is characterized in that the above-mentioned device that irregular heat transfer profile is provided is highly to have variable wall thickness by heat and mass exchange pipe along it to realize.
8. according to each described distilling apparatus of claim 1-2, it is characterized in that the above-mentioned device that irregular heat transfer profile is provided is to have variable cross-section along the height of hot and mass exchange pipe and realize by being arranged on plate on heat and the mass exchange pipe or edge.
9. according to each described distilling apparatus among the claim 1-2, it is characterized in that, it is above-mentioned that the device of irregular heat transfer profile is provided is by realizing around the mozzle of above-mentioned heat and the arrangement of mass exchange pipe, this mozzle is guaranteed and is held certain distance with heat and mass exchange, and punches unevenly along the height of hot and mass exchange pipe.
10. according to each described distilling apparatus among the claim 1-2, it is characterized in that, it is above-mentioned that the device of irregular heat transfer profile is provided is by realizing around the mozzle of above-mentioned heat and the arrangement of mass exchange pipe, this mozzle is guaranteed and is held a radial distance with heat and mass exchange, and the height along heat and mass exchange pipe has irregular interior cross section, and this mozzle top is connected with above-mentioned annular gap with the bottom.
11. according to each described distilling apparatus among the claim 1-2, it is characterized in that, the inner space of above-mentioned heat and mass exchange pipe partly or the heat transfer element of making fully by helix tube fill, the ratio of this helix tube diameter and the heat and the internal diameter of mass exchange pipe be 1:3 to 1:5, helix tube diameter and helix tube length ratio are that 1:1 is to 1:3.
12., it is characterized in that the heat-carrying agent fluid level adjuster in the destilling tower annular gap comprises the outer holding vessel of the heat-carrying agent that is connected with the destilling tower annular gap according to the described distilling apparatus of claim 5.
13., it is characterized in that above-mentioned destilling tower is divided into a plurality of vertical sections according to each described distilling apparatus among the claim 1-2, the inner space of heat and mass exchange pipe is connected between these sections.
14., it is characterized in that each of above-mentioned destilling tower section all has the annular gap that is used for heat-carrying agent of oneself according to the described distilling apparatus of claim 13.
15., it is characterized in that between above-mentioned section, the device that extracts midbarrel being arranged according to the described distilling apparatus of claim 13.
16., it is characterized in that steam and/or fluid flow mutually reduce pro rata in the heat in each continuous segment of destilling tower and the interior cross section of mass exchange pipe and the tower according to the described distilling apparatus of claim 15.
17. according to the described distilling apparatus of claim 2, it is characterized in that, described distilling apparatus comprises a furnace chamber, above-mentioned evaporator has a horizontally disposed heating tube, the inner chamber of above-mentioned heating tube and described furnace chamber are interconnected, tubular space in annular gap between above-mentioned heating tube and the above-mentioned housing and the heat of destilling tower and the mass exchange pipe is connected, and a free space that evaporates phase is arranged at above-mentioned evaporator top by this.
18., it is characterized in that cross section dividing plate with holes is configured in the free space at above-mentioned evaporator top according to the described distilling apparatus of claim 2.
19., it is characterized in that above-mentioned evaporator directly is connected with described furnace chamber according to the described a kind of distilling apparatus of claim 17, destilling tower is arranged in the evaporator zone of contiguous furnace chamber,
For furnace chamber, the input unit of the mixture to be separated of beginning is arranged in the opposite of evaporator, and the residue outlet device is placed in the evaporator bottom zone with the furnace chamber adjacency.
20. according to the described a kind of distilling apparatus of claim 17, it is characterized in that, above-mentioned evaporator is by upright heating tube manufacturing, the inner chamber of described heating tube and destilling tower heat is connected with annular gap with the inner tubular space of mass exchange pipe, and heating tube is connected with described furnace chamber with annular gap between the housing.
21., it is characterized in that above-mentioned destilling tower is arranged in butt end on the above-mentioned evaporator according to the described distilling apparatus of claim 20, above-mentioned furnace chamber utilization distributes annular collector to be connected to the bottom of evaporimeter annular gap.
22., it is characterized in that, second annular collector of an output furnace gas being arranged according to the described distilling apparatus of claim 21 at the top of evaporator annular gap.
23. according to the described distilling apparatus of claim 20, it is characterized in that, above-mentioned evaporator has the input unit of the mixture to be separated of a beginning, this input unit be positioned at tube end sheet on this evaporator above, above-mentioned evaporator also has an output device that is used for residue that is arranged in down below the tube end sheet, therefore, above-mentioned evaporator has a sleeve, and the chamber of sleeve is connected with furnace chamber.
24. according to the described distilling apparatus of claim 22, it is characterized in that, above-mentioned distribution annular collector or above-mentioned second annular collector, or they the two all have respectively around above-mentioned heating tube, and keep the upper and lower dividing plate of annular gap with above-mentioned heating tube.
25., it is characterized in that the heating tube surface between tube end sheet and lower clapboard is by wrapping around above-mentioned heating tube and with protection axle sleeve that heating tube forms annular gap according to the described distilling apparatus of claim 24.
26., it is characterized in that the annular gap between above-mentioned protection axle sleeve and the heating tube is filled by heat-insulating material according to the described distilling apparatus of claim 25.
27. according to the described distilling apparatus of claim 25, it is characterized in that, annular gap between protection axle sleeve and the heating tube is filled by the liquefaction filler, and the filler fusing point is no more than decomposition temperature, and the scope of described decomposition temperature is between substrate mixture decomposition temperature and residue decomposition temperature.
28. according to the described distilling apparatus of claim 24, it is characterized in that, the above-mentioned heating tube surface between the lower and upper dividing plate by the confinement tube of concentric arrangement around.
29., it is characterized in that a sleeve of the device of heating heat-carrying agent is installed in the bottom of destilling tower according to each described distilling apparatus among the claim 1-2.
30. according to each described distilling apparatus among the claim 1-2, a sleeve of the device of heating heat-carrying agent contains the holding vessel of an above-mentioned heat-carrying agent, the last liquid level of holding vessel is below destilling tower.
31. according to each described distilling apparatus among the claim 1-2, it is characterized in that, the above-mentioned heat-carrying agent of the distillation fraction of destilling tower be its boiling point original mixture boiling point to be separated to distillation than any liquid or fluid-mixing between the boiling spread of low boiling constituent element.
32. according to each described distilling apparatus among the claim 1-2, it is characterized in that, above-mentioned tower has stripping part or evaporation section, and the above-mentioned heat-carrying agent that is used for described stripping part or evaporation section is its boiling point at any liquid or the fluid-mixing of original mixture boiling point to be separated in the residue higher constituent element boiling spread.
33., it is characterized in that above-mentioned distribution annular collector has around above-mentioned heating tube according to the described distilling apparatus of claim 21, and keep the upper and lower dividing plate of annular gap with above-mentioned heating tube.
34. be used for evaporimeter tower with heat and mass exchange pipe according to each described distilling apparatus of claim 20-33, it is characterized in that above-mentioned evaporimeter tower has along heat and mass exchange pipe height and the device that provides irregular variable heat to transmit between this pipe inside and outside wall.
35. a kind of according to claim 1-33 in the distil process that fluid-mixing is separated that carries out of each described distilling apparatus, it is characterized in that, between the inside and outside wall of this pipe, carry out irregular variable heat transmission along above-mentioned heat and mass exchange pipe height.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/RU2002/000106 WO2003078014A1 (en) | 2002-03-20 | 2002-03-20 | A compact rectifying unit for separation of mixed fluids and rectifying process for separation of such mixed fluids |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1622846A CN1622846A (en) | 2005-06-01 |
| CN100531842C true CN100531842C (en) | 2009-08-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB02828531XA Expired - Fee Related CN100531842C (en) | 2002-03-20 | 2002-03-20 | Compact distiller unit for separation of mixed fluids and distillation process for separation of such mixed fluids |
Country Status (10)
| Country | Link |
|---|---|
| US (1) | US7588666B2 (en) |
| EP (1) | EP1487553A1 (en) |
| JP (1) | JP2005520670A (en) |
| KR (1) | KR20050014796A (en) |
| CN (1) | CN100531842C (en) |
| AU (1) | AU2002315975A1 (en) |
| BR (1) | BR0215661A (en) |
| CA (1) | CA2476204C (en) |
| MX (1) | MXPA04008942A (en) |
| WO (1) | WO2003078014A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| DE102005023956A1 (en) * | 2005-05-20 | 2006-11-23 | Universität Stuttgart | Compact total evaporator |
| NL1035807C2 (en) * | 2008-08-08 | 2010-02-09 | Pi Productions C V | Method for separating fluid mixture into liquid and vapor in separation chamber, involves subjecting fluid mixture to heat exchange process, performing energy transfer process in fluid mixture, and determining boiling temperature of mixture |
| US8734618B2 (en) * | 2008-12-08 | 2014-05-27 | Shell Oil Company | Apparatus |
| CA2827295A1 (en) * | 2011-02-18 | 2012-11-22 | Heat-Line Corporation | Control for geothermal heating system |
| CN102226487B (en) * | 2011-04-22 | 2012-09-05 | 西安交通大学 | Heat-supply three-layer casing system based on countercurrent heat exchange principle |
| GB2510710B (en) * | 2011-07-01 | 2018-03-21 | Statoil Petroleum As | Multi-phase distribution system, sub sea heat exchanger and a method of temperature control for hydrocarbons |
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| US20240200887A1 (en) * | 2022-12-15 | 2024-06-20 | Raytheon Technologies Corporation | Variable passages to optimize delta p and heat transfer along flow path |
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| DE3706645C2 (en) * | 1987-03-02 | 1988-12-15 | Fa. Doerhoefer Dofa Kessel- Und Apparatebau Gmbh, 8000 Muenchen, De |
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| US5540899A (en) * | 1994-12-22 | 1996-07-30 | Uop | BI-directional control of temperatures in reactant channels |
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2002
- 2002-03-20 JP JP2003576065A patent/JP2005520670A/en active Pending
- 2002-03-20 EP EP02746226A patent/EP1487553A1/en not_active Withdrawn
- 2002-03-20 KR KR10-2004-7014843A patent/KR20050014796A/en not_active Application Discontinuation
- 2002-03-20 CN CNB02828531XA patent/CN100531842C/en not_active Expired - Fee Related
- 2002-03-20 CA CA2476204A patent/CA2476204C/en not_active Expired - Fee Related
- 2002-03-20 WO PCT/RU2002/000106 patent/WO2003078014A1/en active Application Filing
- 2002-03-20 US US10/508,265 patent/US7588666B2/en not_active Expired - Fee Related
- 2002-03-20 AU AU2002315975A patent/AU2002315975A1/en not_active Abandoned
- 2002-03-20 BR BR0215661-0A patent/BR0215661A/en not_active Application Discontinuation
- 2002-03-20 MX MXPA04008942A patent/MXPA04008942A/en active IP Right Grant
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US3530923A (en) * | 1968-05-23 | 1970-09-29 | Metallgesellschaft Ag | Evaporator tubes |
| DE3706645C2 (en) * | 1987-03-02 | 1988-12-15 | Fa. Doerhoefer Dofa Kessel- Und Apparatebau Gmbh, 8000 Muenchen, De |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2476204C (en) | 2011-06-07 |
| WO2003078014A1 (en) | 2003-09-25 |
| EP1487553A1 (en) | 2004-12-22 |
| MXPA04008942A (en) | 2005-06-20 |
| BR0215661A (en) | 2005-02-01 |
| CA2476204A1 (en) | 2003-09-25 |
| AU2002315975A1 (en) | 2003-09-29 |
| US7588666B2 (en) | 2009-09-15 |
| CN1622846A (en) | 2005-06-01 |
| US20050224333A1 (en) | 2005-10-13 |
| KR20050014796A (en) | 2005-02-07 |
| JP2005520670A (en) | 2005-07-14 |
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